Partial oxidation reaction with closed cycle quench

ABSTRACT

The present disclosure relates to a power production system that is adapted to achieve high efficiency power production with complete carbon capture when using a solid or liquid hydrocarbon or carbonaceous fuel. More particularly, the solid or liquid fuel first is partially oxidized in a partial oxidation reactor. The resulting partially oxidized stream that comprises a fuel gas is quenched, filtered, cooled, and then directed to a combustor of a power production system as the combustion fuel. The partially oxidized stream is combined with a compressed recycle CO 2  stream and oxygen. The combustion stream is expanded across a turbine to produce power and passed through a recuperator heat exchanger. The expanded and cooled exhaust stream is scrubbed to provide the recycle CO 2  stream, which is compressed and passed through the recuperator heat exchanger and the POX heat exchanger in a manner useful to provide increased efficiency to the combined systems.

CROSS-REFERENCE TO RELATED APPLICATIONS

The present application claims priority to U.S. Provisional PatentApplication No. 61/597,719, filed Feb. 11, 2012, the disclosure of whichis incorporated herein by reference in its entirety.

FIELD OF THE DISCLOSURE

The present invention is directed to systems and methods for generationof power, such as electricity, that utilize a partial oxidation reactorto achieve high efficiency combustion of a solid fuel. Particularly, thesystem and method can use coal as the solid fuel.

BACKGROUND

Conventional means of power production from combustion of a fueltypically lack the ability to achieve both high efficiency powergeneration and carbon capture and sequestration (CCS) simultaneously.This limitation is magnified when using solid fuels in the combustionreaction because of the solid and inert nitrogen gas contents remainingin the combustion product stream. Accordingly, there is an ever growingneed in the art for systems and methods for high efficiency powergeneration allowing for a reduction in CO₂ emission and/or improved easeof sequestration of produced

One publication in the field of high efficiency power generation withCCS, U.S. Patent Application Publication No. 2011/0179799 to Allam etal. provides one solution whereby a solid fuel such as coal, lignite,pet-coke or biomass is gasified by reaction with oxygen and optionallysteam in a partial oxidation reactor operating at a sufficiently highpressure and temperature to allow substantially complete conversion ofthe solid fuel to a gaseous fuel comprising mainly carbon monoxide andhydrogen as the combustible components together with combustion derivedimpurities, such as H₂S, CS₂, COS, HCN, and NH₃. The partially oxidizednet product gas is cooled, ash is separated, and it is optionallycompressed to allow it to be introduced as fuel into the combustionchamber of the power generation system. The operating pressure of thepartial oxidation system and the power generation system can be suchthat no compression of the fuel gas is required. The power generationsystem combustor operates with an excess of O₂ present followingcombustion, which ensures that the fuel and combustion derivedimpurities are converted from the reduced to their oxidized formscomprising predominantly SO₂ and NO. The partial oxidation reactor canbe provided with transpirationally cooled walls with a high pressurerecycle CO₂ stream cooling the partial oxidation product gas before ashremoval at a temperature level of about 800° C. Further cooling of thepartial oxidation gas to about 400° C. is necessary to ensure that allfine ash particles together with solidified volatile inorganiccomponents are condensed and filtered to prevent solid deposition,corrosion, and blockage of down-stream equipment. The cooling of thepartial oxidation gas from 800° C. to 400° C. must take place in a heatexchanger with tubes for the high pressure partial oxidation gas thatare resistant to metal dusting corrosion due to the Boudouard carbonforming reaction and the high CO partial pressure in the partialoxidation gas. This is shown below in Formula (1).

CO+CO═C+CO₂  (1)

The tubes must be designed to allow periodic water washing to removesolid deposits derived from the condensation of volatile inorganiccomponents present in solid fuels, particularly coal and lignite.

Despite the advances of the above-described publication, the systems andmethods described therein still do not provide a most advantageoussolution to the problems arising when using solid fuels as a powerproduction combustion fuel. Thus, there remains a need for furthersystems and methods for high efficiency combustion of solid fuels withCCS.

BRIEF SUMMARY OF THE DISCLOSURE

The present disclosure provides systems and methods for high efficiencypower production utilizing solid fuels and achieving simultaneous carboncapture. In particular, the disclosed systems and methods can utilize apartial oxidation (POX) reactor wherein the solid fuel is combusted toproduce a POX stream comprising partial oxidation products. The POXstream can be directed to a combustor wherein the at least some of thepartial oxidation products are substantially completely oxidized toproduce a combustion product stream. In certain embodiments, the POXreactor can be operated at pressure that is lower than the pressure inthe combustor.

In specific embodiments, the POX reactor can be can be adapted toutilize a quench cooling fluid. For example, the quench cooling fluidcan be introduced to cool the POX stream from the POX reactiontemperature to a quenched POX stream temperature. In exemplaryembodiments, the ratio of the POX reaction temperature to the quenchedPOX stream temperature can be about 3.25 or greater (e.g., about 3.5:1or about 4:1). As non-limiting examples, the POX reaction temperaturecan about 1300° C. or greater (e.g., about 1300° C. to about 1600° C.),and the quenched POX stream temperature can be at a temperature of about200° C. to about 400° C. The quench cooling can be carried out by directmixing with the POX stream in the POX reactor or a separate vessel.

In other embodiments, solids (such as solid ash particles) producedduring partial oxidation of the primary POX fuel can be removed byseparation from the gaseous fuel gas plus vaporized quench fluid.Alternatively the quench fluid can be present as an additional liquidphase as well as in the gas phase and act as a scrubbing fluid to removethe bulk of the ash particles. A quench temperature of about 400° C. orless can be useful to prevent metal dusting by slowing down theBoudouard reaction where solid carbon is formed from reaction of COmolecules. It further can be preferable to operate the quench system sothat a single phase gaseous POX product with entrained ash particles canbe passed through a cyclone and filter system to remove ash particles.

In further embodiments, the mixture of the POX stream and the quenchcooling fluid vapor can be additionally cooled, such as to a temperatureof about 100° C. or less to provide a cooled POX stream. Quenchingand/or cooling of the POX stream preferably is carried out in a mannersuch that a majority of the useful heat present in the quenched POXstream gas at the POX reaction temperature is recovered. The recoveredheat can be, for example, transferred to the power production system toprovide low temperature heating that can maximize the efficiency of thepower production system, which is further described herein. In someembodiments, part or all of the quench fluid can be separated from thecooled POX stream. The recovered quench fluid can be recycled to the POXreactor.

The disclosed systems and methods are beneficial in that existing,commercially available POX reactors can be adapted for efficientintegration with a power production system. Moreover, the disclosedsystems and methods can be adapted for separation of gaseous products.For example, substantially pure H₂, CO, or mixtures thereof can beseparated from the cooled POX stream. The disclosed systems and methodsfurther are beneficial in that part or all of the fuel and POX-derivedimpurities present in the POX stream can be oxidized in the combustor ofthe power production system. Thereafter, such impurities can be removed(e.g., as acids and salts), such as with a condensed water stream.

In some embodiments, the present disclosure relates to a processcomprising the partial oxidation of a carbonaceous or hydrocarbon fuelby combination with oxygen in a POX reactor. The fuel can include atleast sulfur compounds. The POX reaction can yield a fuel gas mixturecomprising at least H₂, CO, and H₂S. In further embodiments, the POXreaction can yield a fuel gas mixture comprising at least H₂, CO, H₂S,NH₃, and HCN. The POX system can be coupled to a Power Production System(PPS) in which the fuel gas can be combusted with oxygen, and heatenergy formed by the combustion can be converted to power. The methodsutilizing the combined POX system and PPS can be defined by a number ofcharacteristics in various embodiments. Exemplary embodiments areprovided below.

-   -   All impurities derived from the carbonaceous or hydrocarbon        fuel, the POX process, and the oxygen derived from the oxygen        plant (e.g., an air separation unit) that are present in the POX        fuel gas from the POX system following quench cooling, solid ash        removal, and cooling by heat exchange with recycle high pressure        CO₂ from the PPS are combusted in the PPS. Exemplary impurities        can be impurities that are present in excess of H₂, CO, CH₄,        CO₂, H₂O, N₂, and Ar.    -   All oxidizable impurities present in the POX fuel gas can be        oxidized by combustion in the PPS.    -   Sulfur compounds, such as H₂S, COS, and CS₂, that are present in        the POX fuel gas can be oxidized to SO₂, SO₃, H₂O, and CO₂. Any        NH₃ and HCN present in the POX fuel gas can be oxidized to NO,        NO₂, H₂O, and CO₂.    -   The POX process preferably operates at a pressure of about 2 MPa        or greater.    -   The PPS can be defined by generation of power utilizing a        turbine with an inlet pressure of about 10 MPA or greater.    -   The PPS can be defined by generation of power utilizing a        turbine with a pressure ratio of about 12 or less (inlet to        outlet).    -   The POX reaction can be carried out at an adiabatic flame        temperature of about 1300° C. to about 1600° C.    -   The feed to the POX reactor can be slurried with powdered solid        fuel in either water, CO₂, or a combination thereof.    -   The feed to the POX reactor can be defined as comprising an        entrained stream of powdered solid fuel.    -   The feed to the POX reactor can be defined as comprising a        liquid such as a heated stream of bitumen.    -   The POX reactor can be adapted to include an internal heat        transfer section that transfers radiant heat to a portion of a        high pressure recycle stream taken from the PPS at a temperature        of about 250° C. or greater and returned to the PPS at a        temperature below the exit temperature of the high pressure        recycle stream leaving the PPS recuperator heat exchanger.    -   The direct products of the POX reaction can be quench-cooled by        direct mixing with a recycled portion of cooled quenched POX        fuel gas, with a portion of liquid water condensed from the        cooled quenched POX fuel gas, with CO₂ recycled from the PPS, or        with a combination of these three.    -   Ash arising from the fuel used in the POX process can be removed        following quench cooling of the POX products and before further        cooling of the POX fuel gas.    -   The temperature achieved in quench cooling of the POX stream can        be at or below a temperature of about 400° C. or at a        temperature at which the velocity of the BOUDOUARD reaction is        sufficiently low such that no carbon deposition or metal dusting        corrosion occurs in any downstream equipment in the POX system        or the PPS.    -   POX products following quench cooling and ash removal can be        cooled to a temperature of about 100° C. or less by using        heating high pressure recycle fluid streams taken from and        returned to the PPS.    -   The PPS can be defined by the mixing of combustion products in        the PPS combustor with a pressurized recycle stream and the        passage of the total stream through at least one PPS turbine        adapted for power generation.    -   The PPS can be defined by the operation of the turbine or        turbines at a final discharge pressure of about 0.1 MPa or        greater or, in other embodiments, about 1 MPa or greater.    -   The PPS can be defined by the use of one or more recuperative        heat exchangers that heat the previously compressed high        pressure recycle stream against at least the total turbine        exhaust stream or streams.    -   The PPS can be defined by the conversion of the SO₂ and SO₃ to        H₂SO₄ by reaction with O₂, liquid H₂O, NO₂, and NO.    -   The PPS can be defined by the conversion of NO, NO₂, and liquid        H₂O to HNO₃.    -   The PPS acid conversions can be carried out at an operating        temperature corresponding to the point at which water condenses,        down to a temperature at which the water and acids are separated        from the cooled turbine exhaust gas at the cold end of the        recuperative heat exchanger.    -   Acids plus soluble inorganic components formed by reaction with        the acids and optionally diluted with condensed water from the        PPS combustor can be removed for further treatment.    -   A high pressure CO₂ recycle fluid stream or streams can be used        for cooling the quenched POX product gas following ash removal.    -   The high pressure CO₂ recycle fluid stream can optionally        comprise more than one fluid stream taken from the PPS at more        than one temperature level.    -   More than one high pressure CO₂ recycle fluid stream can be        returned to the PPS at more than one temperature level.    -   One fluid stream can be taken from the PPS and returned to the        PPS as more than one stream at more than one temperature level.    -   More than one fluid stream can be taken from the PPS and        returned to the PPS as a single heated stream.    -   The cooled net POX fuel gas product, following cooling and        separation of POX quench recycle fluid, can be compressed from        the pressure at which it exits the POX system to a pressure        substantially the same as the inlet pressure of the PPS        combustor.    -   A fluid stream taken from the PPS for use in cooling a quenched        POX product gas can be part of the pressurized recycle stream        from the PPS.    -   The oxygen used in the POX system can have a purity greater than        90% molar, preferably greater than 95% molar.    -   The partially oxidized gas can be quenched with water producing        a gas mixture containing at least H₂, CO, CO₂, one or more        sulfur compounds (e.g., H₂S), and H₂O.    -   Cooling of the quenched POX fuel gas can be carried out with two        streams of pressurized recycle gas from the PPS; the inlet        temperature of the first recycle stream entering the POX heat        exchanger can be at the discharge temperature of the PPS recycle        CO₂ compressor; and the inlet temperature of the second recycle        CO₂ stream entering the POX heat exchanger can be within 20° C.        of the water dew-point in the PPS turbine exhaust stream.    -   The POX stream comprising fuel gas can be quenched with water to        produce a POX gas saturated with water vapor having excess        liquid water present; and the two inlet streams of pressurized        recycle gas from the PPS can leave the POX heat exchanger as a        single stream at a temperature within 20° C. of the POX gas        dew-point temperature.    -   The POX stream can be quenched with water to produce a quenched        POX stream that is above its dew-point temperature and below        400° C.; the two inlet streams entering the POX heat exchanger        can be heated and combined at the temperature point        corresponding to the second inlet stream temperature; a first        exit heated fluid stream can be removed at a temperature within        20° C. of the POX stream dew-point temperature, and the        remaining stream can be further heated and leave the POX heat        exchanger at a temperature of about 380° C. to 399° C.    -   A portion of the POX fuel gas following quench cooling can be        removed and passed through a catalytic shift reactor to convert        CO and H₂O to H₂ and CO₂.    -   The exit gas from the shift reactor can be cooled in the        quenched POX heat exchanger against recycle gas taken from and        returned to the PPS.    -   The shifted gas can be mixed with a portion of the un-shifted        gas and further processed to separate water, CO₂, sulfur        compounds, mercury, and other volatile inorganic components,        leaving a mixture comprising H₂ and CO in a ratio from 0.8 to 1        to 2.5 to 1.    -   The shifted gas alone can be further processed to produce a pure        H₂ stream of greater than 99% molar.    -   The content of sulfur compounds, NH₃, HCN, and water in the H₂        or H₂ and CO streams each can be less than 1 ppm molar.    -   The separation device can be defined as a multi-bed pressure        swing adsorption (PSA) system.    -   The low pressure waste gas from the PSA comprising the adsorbed        products from the PSA system can be compressed to the pressure        required by the PPS combustor and mixed into the total POX fuel        gas flow to the PPS combustor.    -   The oxygen used for the POX of the primary fuel can be heated in        the POX heat exchanger to a temperature of up to 350° C.    -   The oxygen used in the PPS combustor can be heated in the POX        heat exchanger to a temperature of up to 350° C.

In some embodiments the present disclosure can relate to a process forthe production of power using a combination of a POX system and a PPS,and the process can comprise the following steps:

combining a solid or liquid fuel and oxygen in a POX reactor underconditions sufficient to partially oxidize the fuel and form a POXstream comprising a fuel gas;

-   -   quenching the POX stream through combination with a quenching        fluid under conditions sufficient to form a quenched POX stream        at a temperature of about 400° C. or less and to solidify at        least a portion of any molten solids present in the POX stream;

treating the quenched POX stream so as to remove at least a portion ofany solids present therein;

directing the quenched POX stream to a POX heat exchanger andwithdrawing a quantity of heat from the quenched POX stream by coolingthe quenched POX stream to a temperature of about 100° C. or lessagainst a cooling stream and form a POX fuel gas stream;

passing the POX fuel gas stream through a separator vessel andseparating at least a portion of any water present in the POX fuel gasstream;

compressing the POX fuel gas stream to a pressure of about 12 MPa orgreater;

combusting the POX fuel gas in a PPS combustor to form a combustionproduct stream (optionally with a portion of excess oxygen) at apressure of at least about 10 MPa and a temperature of at least about800° C.; and

expanding the combustion product stream across a PPS turbine to generatepower and form an expanded PPS combustion product stream.

In specific embodiments, the process for the production of power can befurther defined by a variety of characteristics that may beindependently applied to a process as noted above. For example, thesolid or liquid fuel can be a carbonaceous fuel. The fuel combined inthe POX reactor can be an entrained stream of a powdered, solid fuel.The carbonaceous fuel specifically can be coal. The coal can be slurriedwith water or CO₂. The quenched POX stream can comprise ash, slag, or acombination thereof, and the step of removing solids can comprisepassing the quenched POX stream through a water scrubber unit. The stepof removing solids can comprise filtering the quenched POX stream so asto reduce dust load to about 4 mg or less per cubic meter of fuel gas inthe quenched POX stream. The POX reactor can be operated at a POXtemperature, and a ratio of the POX temperature to the temperature ofthe quenched POX stream can be about 2:1 or greater. The POX temperaturecan be about 1300° C. to about 1600° C. The POX reactor can be operatedat a pressure of about 2 MPa or greater. Quenching can comprise mixingthe POX stream with: a recycled portion of the cooled POX fuel gasstream exiting the heat exchanger; a portion of the water separated fromthe cooled POX fuel gas stream; CO2 recycled from the PPS, water, or acombination thereof. The cooling stream in the heat exchanger cancomprise a high pressure recycle fluid stream withdrawn from andreturned to the PPS. The high pressure recycle fluid stream can be arecycle CO₂ fluid stream. The recycle CO₂ fluid stream can comprise CO₂formed in the combusting of the POX fuel gas in the PPS combustor. ThePOX reactor can include an internal heat transfer component. Theinternal heat transfer component can be adapted to transfer radiant heatto a portion of a high pressure recycle stream taken from a component ofthe PPS at a temperature of about 250° C. or greater. The internal heattransfer component can be adapted to return the high pressure recyclestream to a component of the PPS. The PPS turbine can have an inletpressure of about 10 MPa or greater. The PPS turbine can have an outletpressure that is defined as a ratio of the turbine inlet to the turbineoutlet. In an example embodiment, the ratio can be about 10 or less.

In further embodiments, the process for the production of power using acombination of a POX system and a PPS also can comprise:

passing the expanded PPS combustion product stream through a PPSrecuperator heat exchanger and thereby withdrawing heat from the PPScombustion product stream and forming a cooled PPS combustion productstream;

optionally passing the cooled PPS combustion product stream through awater cooler;

treating the cooled PPS combustion product stream in a PPS scrubberseparating at least one or H₂SO₄, HNO₃, or water-dissolved Hg salts andforming a recycle CO₂ stream; and

pressurizing the recycle CO₂ stream in a PPS compressor and forming acompressed recycle CO₂ stream.

In specific embodiments, the separating step can comprise separatingconversion products H₂SO₄ and HNO₃ formed by reaction of SO₂, SO₃, NO,NO₂, H₂O, and O₂ plus condensed water and dissolved Hg salts. Passingthe expanded PPS combustion product stream through the PPS recuperatorheat exchanger can cool the PPS combustion product stream to atemperature below the water dew point. The fuel gas in the POX fuel gasstream entering the PPS combustor can comprise at least one fuel gascomponent selected from H₂, CO, and CH₄. The POX fuel gas streamentering the PPS combustor can comprise one or more impurities separatefrom the fuel gas and derived from the solid or liquid fuel, the partialoxidation thereof, and the oxygen. The one or more impurities cancomprise at least one of a sulfur compound, NH₃, and HCN. The one ormore impurities expressly can exclude N₂ and argon. Substantially all ofthe impurities can still be present in the POX fuel gas stream and canbe combusted in the PPS combustor. All oxidizable impurities present inthe POX fuel gas stream can be oxidized by the combustion in the PPScombustor. The combustion product stream from the PPS combustor cancomprise a mixture of combustion products and at least a portion of thecompressed recycle CO₂ stream. The withdrawn heat from the PPScombustion product stream can heat at least a portion of the compressedrecycle CO₂ stream. The POX stream can be quenched with water. The waterquenched POX stream can comprise at least H₂, CO, CO₂, H₂S, and H₂O. Thecooling stream in the POX heat exchanger can comprise two streams of thecompressed recycle CO₂. An inlet temperature of the first compressedrecycle CO₂ stream entering the POX heat exchanger can be substantiallythe same as a temperature of the compressed recycle CO₂ streamdischarged from the PPS compressor. An inlet temperature of the secondcompressed recycle CO₂ stream entering the POX heat exchanger can bewithin 20° C. of the water dew-point in the expanded PPS combustionproduct stream. The water quenched POX stream can be saturated withwater vapor so as to comprise excess liquid water. The two compressedrecycle CO₂ streams can combine in the POX heat exchanger to form asingle stream. The single compressed recycle CO₂ stream exiting the POXheat exchanger can be at a temperature that is within about 20° C. ofthe POX fuel gas dew-point temperature. The water quenched POX streamcan have a temperature that is above its dew-point temperature and belowabout 400° C. The two compressed recycle CO₂ streams can be heated, andthe point at which the two compressed recycle CO₂ streams combine toform the single stream can be at a temperature that substantiallycorresponds to the inlet temperature of the second compressed recycleCO₂ stream. The single stream can be split into the following: a firstexiting heated and compressed recycle CO₂ stream that exits the POX heatexchanger at a temperature that is within about 20° C. of the POX streamdew-point temperature; and a second exiting heated and compressedrecycle CO₂ stream that exits the POX heat exchanger at a temperature ofabout 380° C. to about 399° C.

In additional embodiments, a portion of the quenched POX stream can bedirected through a POX catalytic shift reactor. The POX catalytic shiftreactor can be adapted to convert a mixture of CO and H₂O into a shiftreactor exit gas comprising a mixture of H₂ and CO₂. The shift reactorexit gas can be cooled in the POX heat exchanger against a recycle gastaken from and returned to the PPS. The shift reactor exit gas can bemixed with a portion of the quenched POX stream and can be furtherprocessed to separate water, CO₂, sulfur compounds, Hg, and volatileinorganic compounds so as to form a mixture comprising H₂ and CO in aratio of about 0.8:1 to about 2.5:1. The shift reactor exit gas can befurther processed to form a pure H₂ stream with a purity of 99% orgreater molar. The POX stream processor can be a multi-bed pressureswing adsorption (PSA) system. A low pressure waste gas from the PSAsystem comprising adsorbed products from the PSA system can becompressed to a PPS combustor pressure and mixed into a total fuel gasflow entering the PPS combustor. The oxygen used in the POX reactor canbe heated in the POX heat exchanger to a temperature of up to about 350°C. The oxygen used in the PPS combustor can be heated in the POX heatexchanger to a temperature of about 350° C.

In other embodiments, the present disclosure can provide a combined POXsystem and PPS, and the combined system can be useful for producingpower, such as electricity, from a starting fuel that is non-gaseous. Insome embodiments, a POX system and PPS can comprise the followingelements:

a POX reactor adapted to partially oxidize a liquid or solid fuel in thepresence of oxygen to form a POX stream comprising a fuel gas;

one or more components adapted to contact the POX stream with aquenching fluid;

an optional POX scrubber adapted to separate any solids present in thequenched POX stream from the POX fuel gas;

a POX heat exchanger adapted to withdraw heat from the POX fuel gasagainst a portion of a compressed recycle CO₂ stream and output a cooledPOX fuel gas;

an optional separator adapted to separate any liquid water from the POXfuel gas;

a compressor adapted to compress the cooled POX fuel gas to a pressureof about 12 MPa or greater;

a PPS combustor adapted to combust the POX fuel gas in the presence ofoxygen and a portion of the compressed recycle CO₂ stream and form a PPScombustion product stream at a pressure of about 12 MPa or greater;

a turbine adapted to expand the PPS combustion product stream andgenerate power in a connected generator;

a recuperator heat exchanger adapted to withdraw heat from the expandedPPS combustion product stream and add the heat to the compressed recycleCO₂ stream;

a PPS scrubbing tower adapted to separate any oxidized impurities fromthe expanded PPS combustion product stream and output a recycle CO₂stream;

a PPS compressor adapted to compress the recycle CO₂ stream to apressure of about 12 MPa or greater and form the compressed recycle CO₂stream;

flow components adapted to direct a portion of the compressed recycleCO₂ stream to the POX heat exchanger;

flow components adapted to direct a portion of the compressed recycleCO₂ stream to the PPS recuperator heat exchanger; and

flow components adapted to direct the compressed recycle CO₂ stream fromthe POX heat exchanger to the PPS recuperator heat exchanger.

BRIEF DESCRIPTION OF THE DRAWINGS

Having thus described the invention in general terms, reference will nowbe made to the accompanying drawings, which is not necessarily drawn toscale, and wherein:

FIG. 1 is flow sheet illustrating an example embodiment of a combinedPOX system and PPS according to the present disclosure wherein the PPSgenerates power using a fuel gas derived from the partial oxidation of aliquid or solid hydrocarbon or carbonaceous fuel in the POX system;

FIG. 2 is a flow sheet illustrating a portion of the combined systemfrom FIG. 1, wherein the illustrated portion particularly shows elementsof the combined system useful for production of export H₂ or H₂+COmixtures;

FIG. 3 is a plot of temperature versus heat transferred in a fuel gasheat exchanger for a system according to an example embodiment of thepresent disclosure using a CO₂ coal slurry with a water quenched POXreaction operating with excess water so that the quenched POX fuel gasis at the water dew-point temperature;

FIG. 4 is a plot of temperature versus heat transferred in a POX heatexchanger for a system according to an example embodiment of the presentdisclosure using a CO₂ coal slurry with a water quenched POX reactionoperating at a quench temperature of 400° C.;

FIG. 5 shows the mass and heat balance from an ASPEN simulation of apower system combining a POX system and a PPS according to an exampleembodiment of the present disclosure, wherein the simulation includedthe use of a coal/CO₂ slurry in the POX reactor and utilization of wateras a quenching fluid; and

FIG. 6 shows the mass and heat balance from an ASPEN simulation of apower system combining a POX system and a PPS according to an exampleembodiment of the present disclosure, wherein the simulation includedthe use of a coal/CO₂ slurry in the POX reactor and utilization of CO₂as a quenching fluid.

DETAILED DESCRIPTION OF THE DISCLOSURE

The invention now will be described more fully hereinafter throughreference to various embodiments. These embodiments are provided so thatthis disclosure will be thorough and complete, and will fully convey thescope of the invention to those skilled in the art. Indeed, theinvention may be embodied in many different forms and should not beconstrued as limited to the embodiments set forth herein; rather, theseembodiments are provided so that this disclosure will satisfy applicablelegal requirements. As used in the specification, and in the appendedclaims, the singular forms “a”, “an”, “the”, include plural referentsunless the context clearly dictates otherwise.

The systems and methods of the present disclosure are adapted forachieving partial oxidation (POX) of a carbonaceous fuel, particularly asolid fuel and/or a liquid fuel. Non-limiting examples of fuels that canbe used according to the present disclosure include coal, lignite,petroleum coke, bitumen, biomass, algae, wood, graded combustible solidwaste refuse, asphalt, used tires, crude oil, other ash containingliquid fuels, and the like.

In various embodiments, the systems and methods of the disclosure areadapted to partially oxidize the fuel using oxygen, preferablysubstantially pure O₂, so as to produce a stream that is useful as afuel gas. The partial oxidation can be carried out in a POX reactor. Inparticular embodiments, an air separation unit or other oxygen plant canbe utilized in the systems and methods of the present disclosure. Oxygenfrom the plant can be directed to the POX reactor. In some embodiments,the oxygen can be first passed through a heat exchanger to increase thetemperature of the oxygen entering the POX reactor. Nitrogen from theair separation plant also can be incorporated into the systems andmethods. For example, dry N₂ can be passed through a crusher that isparticularizing solid fuels and thus partially dry the particulate fuel.The particulate fuel can be further crushed in a second crusher to aparticle size preferably of about 500 microns or less, about 250 micronsor less, or about 100 microns or less. The small particle fuel can bedirected to a mixer to be formed into a slurry with a slurrying medium.The slurry medium can comprise CO₂, which preferably has a pressure ofabout of 3.5 MPa or greater, about 5 MPa or greater, or about 8.5 MPa orgreater. The CO₂ in the CO₂ slurry medium preferably can be at atemperature of about 5° C. to about 40° C., about 10° C. to about 30°C., or about 12° C. to about 25° C. The CO₂ in the CO₂ slurry medium canhave a density of about 500 kg/m³ to about 1000 kg/m³, about 600 kg/m³to about 900 kg/m³, or about 700 kg/m³ to about 800 kg/m³. The slurrymedium can alternately comprise water or a combination of CO₂ and water.A solid fuel slurry used in the POX reactor can comprise about 25% toabout 75%, about 30% to about 70%, or about 40% to about 60% by weightsolid fuel. The particulate fuel slurry is then combined in the POXreactor with the oxygen, which preferably comprises about 90% molar orgreater, about 95% molar or greater, of about 97% molar or greateroxygen. The POX reactor preferably operates at a pressure of about 4.5to about 8.5 MPa and a temperature of about 1450° C.; however, thetemperature and pressure can be in any combinations of temperature andpressure ranges as otherwise disclosed herein in relation to the natureof the POX stream exiting the POX reactor.

Partial oxidation of the carbonaceous fuel in the POX reactor forms aPOX stream, which can be defined in terms of the components thereof. Inparticular, the POX stream can comprise a fuel gas and one or moreimpurities (oxidizable impurities and non-oxidizable). The fuel gas cancomprise hydrogen, carbon monoxide, or a combination thereof. Exemplaryimpurities derived from the original POX fuel (solid or liquidhydrocarbons or carbonaceous material) or the partial oxidationreactions include, for example, H₂S, COS, CS₂, HCN, NH₃, and Hg. Thestream arises from the POX reactor wherein the POX stream producedtherefrom can be quenched with a cooling fluid. This can result in thepartial vaporization of the cooling fluid to produce a fuel gascomprising vaporized cooling fluid mixed with fuel gas. Excess quenchcooling fluid can be used giving a mixture of liquid cooling fluid andvapor fuel gas plus vaporized cooling fluid as a product from the POXreactor. The cooled POX stream can undergo separation so that solids(e.g., solid ash particles) can be removed. The solids particularly canbe removed in a mixture with the liquid cooling fluid that is separatedfrom the fuel gas mixture. Any remaining fine ash particles can beremoved by a downstream cooling fluid wash column followed by a candlefilter or the like. Alternatively, the quench can result in a gaseousphase with entrained ash particles that are removed in a combination ofcyclones and filters. The cooled POX stream thereafter can be cooled ina heat exchanger to recover at least a portion of the useful heat thatwas present in the POX stream prior to quench cooling. In particular,the bulk of the vaporized cooling fluid mixed with the fuel gas can becondensed, and the heat can be transferred primarily to a high pressurerecycle stream to reduce the temperature difference at the hot end of arecuperative heat exchanger in the power production system. This can beparticularly beneficial to increase the overall efficiency of the powerproduction system alone or in combination with the POX system. The POXstream (i.e., the fuel gas stream) can be produced at a pressure that isless than or equal to the pressure required for further combustion ofthe fuel gas in the combustor for power production. For example, acombustor and associated power production cycle that can be combinedwith the systems and methods of the present disclosure is described inU.S. Patent Application Publication No. 2011/0179799, the disclosure ofwhich is incorporated herein by reference in its entirety. Suchcombustor and associated power production cycle may be referenced hereinas the “NET Power System.” The process of the NET Power System achievespower generation using predominantly CO₂ as a working fluid. Inparticular, the process uses a high pressure/low pressure ratio turbinethat expands a mixture of a high pressure recycle CO₂ stream andcombustion products arising from combustion of the fuel. Pure oxygen canbe used as the oxidant in the combustion process. The hot turbineexhaust is used to partially preheat the high pressure recycle CO₂stream. The recycle CO₂ stream of the NET Power System is also heatedusing heat derived from the compression energy of the air feed of the O₂production plant. All fuel and combustion derived impurities such assulfur compounds, NO, NO₂, CO₂, H₂O, Hg and the like are separated fordisposal with no emissions to the atmosphere.

The systems and methods of the present disclosure specifically can becharacterized as being a combination of a POX system and powerproduction system (PPS). The NET Power system is an example of a PPSthat can be used according to the present disclosure. In particular, aPOX fuel gas stream can be introduced to the PPS combustor as part orall of the fuel stream for the combustor. In a high pressure combustioncycle, the fuel gas from the POX stream must in general be compressed tothe high pressure required in the power production system combustor. Forexample, the POX fuel gas stream may be compressed in a compressor to apressure of at about 10 MPa or greater, about 15 MPa or greater, about20 MPa or greater, or about 25 MPa or greater. In other embodiments, thepressure can be about 8 MPa to about 50 MPa, about 15 MPa to about 45MPa, or about 20 MPa to about 40 MPa.

The POX fuel gas stream arising from the reaction of the oxygen with asolid or liquid fuel can comprise varying amounts of solids and moltensolids that must be removed before introduction of the POX fuel gasstream into the PPS combustor. Specifically, the POX fuel gas stream canbe quenched and cooled as necessary to a temperature wherein ash andother solid materials can be removed. This is beneficial to preventdownstream contamination of equipment in the POX system and the PPS. Theheat liberated during cooling of the POX fuel gas stream can betransferred to the power production system to maximize overallefficiency of the power production system. In particular, this heat canbe used for partially heating at least a portion of the recycle CO₂fluid circulating in the power production after cooling of thecombustion product stream and prior to input of the recycle CO₂ fluidback into the combustor of the power production system. In particular,the heat can be added to the recycle CO₂ fluid following the compressionof the recycle CO₂ fluid. Optionally the oxygen required for the POXreactor and/or the power production system combustor can also be heatedagainst the cooling POX stream in the same or a different heatexchanger.

The POX reactor can be adapted to provide an output POX fuel gas streamhaving a temperature that is about 1200° C. or greater, about 1300° C.or greater, or about 1400° C. or greater. More particularly, thetemperature can be about 1000° C. to about 2000° C., about 1200° C. toabout 1800° C., or about 1300° C. to about 1600° C. In variousembodiments, one or more steps can be utilized to cool the POX stream(and thus the fuel gas for input to a further combustor), preferably toabout ambient temperature.

In one step, the POX stream immediately exiting the POX reactor at atemperature as described above can be quenched to a lesser temperature.Quenching reduces the temperature preferably to 400° C. or less which isa region where the velocity of the BOUDOUARD reaction is so low that nocarbon formation or metal dusting corrosion will occur. Quenching to atemperature of 400° C. or less serves to condense volatile metal saltsfor subsequent removal. The quenching step can be adapted to reduce thetemperature of the POX stream to a lesser temperature that can bedefined by a ratio in relation to the POX reaction temperature. Inparticular embodiments, the ratio of the POX reaction temperature to thetemperature of the quenched POX stream can be about 3.25:1 or greater,about 3.5:1 or greater, or about 4:1 or greater. More particularly, thetemperature ratio of the POX stream to the quenched POX stream can beabout 3.25:1 to about 6:1, about 3.75:1 to about 5.5:1, or about 4:1 toabout 5:1. In particular embodiments, the temperature of the quenchedPOX stream can be about 400° C. or less, about 350° C. or less, or about300° C. or less. In particular embodiments, the temperature can be about200° C. to about 400° C., about 225° C. to about 375° C., or about 250°C. to about 350° C. Quenching can be carried out by mixing of the POXstream with one or more quenching fluids. Non-limiting examples ofquenching fluids that can be used according to the present disclosureinclude a stream of recycled POX product (i.e., at least a portion ofthe POX product that has been already cooled to a quenching fluidtemperature then cooled in the POX gas heat exchanger followed by liquidwater separation), water at a quenching fluid temperature, liquid CO₂,mixtures thereof, and the like. A useful quenching fluid temperature canbe about 150° C. or less, about 100° C. or less, about 75° C. or less,or about 60° C. or less. The quenching fluid temperature particularlycan be about 10° C. to about 150° C., about 15° C. to about 100° C., orabout 20° C. to about 75° C. Alternately the quenching fluid can bepreheated against the cooling quenched POX gas or by other means to atemperature approach of typically about 20° C. below the POX quenchtemperature. In embodiments using a water quench, a portion of the watercan be vaporized thus giving a mixture of fuel gas, steam, and a liquidwater portion, which washes out the bulk of the ash particles. Thetemperature of the total liquid and vapor will be determined by thepressure used in the POX reactor and the quantity of liquid water usedfor the quench.

A further step can provide for separation of any liquid water and thebulk of any ash particles or further solids from the quenched POX streamvapor. Removal of the solids can be carried out using any conventionalseparation or filter means. Non-limiting examples of suitable solidsremoval components include cyclone filters, settling tanks, candlefilters, bag filters, liquid wash towers, and the like. In someembodiments, a separator can be provided in the lower part of the POXreactor. The separated vapor in general can be introduced into the baseof a counter current water wash column to remove further traces ofparticulate ash. The cleaned POX fuel gas plus steam stream can thenoptionally be passed through a gas filter, such as a candle filter, toensure that there can be no deposition of particles in the heatexchanger used for cooling the fuel gas or in the downstream PPS. Insome embodiments, a liquid CO₂ stream can be used as the quench fluid.In this case the total stream after quench may consist of a single vaporphase with entrained solid particles. The quantity of liquid CO₂ usedfor quench can be such that the temperature of the quenched stream isabout 200° C. to about 400° C. The ash can be removed in a series offilters as noted above. In other embodiments, a cooled separated fuelgas stream following water separation can be used as part or all of thequench fluid. In various embodiments, a preferred method of quench mayuse water. The system may also use a mixture of water and CO₂ in whichthe quantity of water is sufficient to produce enough liquid waterfollowing quench to wash out the bulk of the ash particles.

In yet another step, the quenched POX stream (preferably after filteringof solids) can be cooled to near ambient temperature. Accordingly, thedisclosed systems and methods can include one or more components adaptedfor heat exchange. In particular, a heat exchanger can be adapted totransfer the heat from the quenched POX stream to one or more portionsof the high pressure CO₂ recycle stream utilized in the power productionsystem. For example, the heat can be transferred to the high pressureCO₂ recycle stream taken from the CO₂ recycle compressor dischargeand/or to one or more appropriate points in the recuperator heatexchanger that is used in the power production cycle. The choice oftemperatures for the injection of heat to the PPS recuperator heatexchanger and the number and inlet temperature of the streams taken fromthe PPS recuperator heat exchanger to be heated in the quenched fuel gascooler can be determined by altering the heat recovery process to ensureheat recovery is at the maximum temperature level consistent witheconomic heat exchanger sizes.

The solid fuel used in the POX reactor can be provided in a variety offorms. In embodiments noted above, a solid fuel can be provided in aparticulate form, preferably a finely powdered state and can be slurriedwith a slurry medium. In preferred embodiments, the slurry medium cancomprise, for example, water, liquid CO₂, and combinations thereof.Liquid CO₂ can be formed, at least in part, from recycled CO₂ from thepower production system. The use of CO₂ as the slurrying fluid can beparticularly useful to reduce the heat required to raise the temperatureof the POX fuel feed to the POX reactor range as compared to the use ofa different slurry medium such as water (e.g., water condensed andseparated from the power production system). Although CO₂ can be apreferred slurrying medium, other materials, including water, may stillbe used as desired and may lead to acceptable losses in efficiency undercertain embodiments of the present disclosure. The carbonaceous fuelused in the POX reactor can be a liquid such as heated bitumen, in whichcase no slurrying fluid may be needed.

When using CO₂ or water as the slurrying medium, the composition of thePOX stream leaving the POX reactor can have a high carbon monoxide (CO)concentration and partial pressure. In such embodiments, it can beparticularly desirable to ensure that quenching of the POX stream isadapted to cool the stream and thus form a quenched POX stream having atemperature of less than 400° C. Providing such temperature drop canparticularly limit BOUDOUARD reaction kinetics to a sufficiently lowstate such that no carbon can be deposited in the POX stream heatexchanger and such that no metal dusting corrosion can take place indownstream equipment.

In relation to particular embodiments, the systems and methods of thedisclosure can encompass at least the following four sets of operatingconditions in relation to the combination of the POX fuel feed and thePOX heat exchange: CO₂ fuel slurry with CO₂ quench; CO₂ fuel slurry withwater quench; water fuel slurry with water quench; and water fuel slurrywith CO₂ quench. It is understood, however, that other combinations mayarise based upon utilization of further slurrying media and/or furtherquenching fluids. Moreover, the fuel slurry medium can be a combinationof water and CO₂. Likewise, the quenching fluid can be a combination ofwater and the cooled POX stream.

Heat liberated by cooling the quenched POX stream in the heat exchangerfollowing ash removal can be transferred to one or more portions of thehigh pressure CO₂ recycle stream taken from the power production system.The quench fluid can be recycled POX fuel gas leaving the cool end ofthe POX heat exchanger following liquid water separation, or it can becondensed and separated water. It also can be a combination of fuel gasand water. Still further, it can be recycled CO₂, or a combination offuel gas, or water, or both with CO₂. In some embodiments, the source ofthe quench fluid can be particularly relevant. Embodiments utilizing aCO₂ slurrying medium can result in a net production of water derivedfrom hydrogen and water present in the solid fuel feed (e.g., coal).Separated liquid water thus can be treated to separate flammablecomponents dissolved in the water. These separated flammables can becompressed and returned to the power production system combustor. Thecleaned water stream then can be recycled to either the solid fuelslurrying system or the POX quench system, and any surplus water can besent to the power production system where it can be used to dilute anyH₂SO₄/HNO₃ acid produced at the water separation stage in the powerproduction system as described in U.S. Patent Application PublicationNo. 2011/0179799. In embodiments wherein the solid fuel is slurried withwater, the water present in the high temperature POX stream can reactwith the CO produced by partial oxidation of the carbon in the solidfuel to produce hydrogen gas and carbon monoxide. These can be presentin a ratio of approximately 1:1 H₂ and CO by volume.

This consumption of water in the shift reaction can be indicative of awater deficiency, and water produced in the power production system thencan be returned to the POX system to produce the solid fuel coal slurryand thus make up for this consumption. The net, cooled POX stream (i.e.,the fuel gas stream) then can be compressed to the required pressure forcombustion in the power production combustor. In various embodiments,the system and method of the present disclosure can be adapted forproduction of an internal quench fluid for use with the high temperaturePOX stream exiting the POX reactor. This can arise from the sequentialsteps of POX reaction, solids removal, heat exchange cooling, and waterseparation. The net quantity of fuel gas from the POX stream can becompressed and delivered to the power production system combustor with arelatively high concentration of flammable gases (e.g., H₂ and CO) andwith a calorific value which will ensure useful combustion conditions inthe power production system combustor.

In some embodiments, a POX reactor according to the disclosure can beadapted to operate at a pressure that is higher than the pressure in thepower production system combustor. The power production system combustorparticularly can use CO₂ as the working fluid that is continuouslyrecycled in the system. Preferably, the POX stream can be quenched andcooled via heat exchange as described herein using either cooled POXstream or water as the quench medium, and the cooled POX stream (i.e., afuel gas) can be used in the power production system without the needfor further compression. The POX reactor can comprise any reactoradapted for combustion of a carbonaceous fuel, particularly wherein thefuel is only partially oxidized, and particularly wherein the reactor isadapted to function at a pressure that is greater than the operatingpressure of a power production system combustor as described herein. Inexemplary, non-limiting embodiments, a POX combustor can utilizetranspiration cooling wherein a cooling fluid, such as CO₂, is passedthrough a porous transpiration layer surrounding the POX combustionchamber, which can be particularly useful to prevent ash impingement andagglomeration. Exemplary embodiments of transpiration cooling that canbe used with a POX reactor according to the present disclosure aredescribed in U.S. Patent Application Publication No. 2010/0300063 toPalmer et al., U.S. Patent Application Publication No. 2011/0083435 toPalmer et al. and U.S. Patent Application Publication No. 2012/0073261to Palmer et al., the disclosures of which are incorporated herein byreference in their entireties.

In further embodiments, a POX reactor according to the disclosure can beadapted to operate at a pressure that is below the pressure of the powerproduction system combustor. In such embodiments, a POX stream for useas a fuel in the power production system combustor can be compressedbefore passage into the power production system combustor. The POXreactor can comprise any commercially available system. Non-limitingexamples of commercially available systems useful according to thepresent disclosure include a Shell dry powdered coal feed entrained flowreactor, a GE/Texaco quench reactor, a Siemens cooling screen quenchreactor, or similar systems. Useful POX reactors can include internalheat transfer sections absorbing radiant heat from the POX burner. Insuch embodiments, a portion of the high pressure recycled CO₂ streamfrom the power production system can be heated and returned at a highertemperature to the PPS system. For example, recycled CO₂ at atemperature of about 400° C. or higher can be heated to a temperature ofabout 450° C. to about 600° C. within the POX reactor and returned tothe recuperative heat exchanger in the power production system where itcan be remixed with a further portion of the high pressure recycle CO₂stream at a similar temperature.

Combination of a POX reactor with a power production system according tothe present disclosure can provide a variety of useful aspects. As anexample, the combination can be defined in that impurities (such as fromcoal or other solid fuel and from partial oxidation of the fuel) can beretained in the cooled, high pressure POX stream that enters the powerproduction system combustor. Such impurities can comprise H₂S, COS, CS₂,HCN, NH₃, Hg. These and other impurities can be oxidized in the powerproduction system combustor so as to form, for example, SO₂, CO₂, N₂,NO, and Hg, which then can be removed from the power production system.For instance, a water stream condensed from the power production systemcombustor exit stream can be acidic comprising one or more of HNO₃,H₂SO₄, and dissolved inorganic salts, such as described in U.S. PatentApplication Publication No. 2011/0179799.

The processing of the solid fuel through the POX reactor rather thandirectly through a power production system combustor can be particularlyuseful in light of the ability to remove possibly fouling reactionproducts. For example, a POX stream exiting the POX reactor can bequenched to a temperature of about 400° C. or less or a furthertemperature useful to ensure that ash derived from coal (or other moltenimpurities arising from coal or other solid fuel) is in a solid formwhich can be removed. Preferably, solid impurities can be removed downto a very low concentration and sufficiently low particle size so as tosubstantially prevent blockage and/or corrosion of components of thepower production system, such as heat exchangers, turbines, compressors,and the like.

In addition to the foregoing, the quenching of the POX stream from thePOX reactor can be adapted to provide a quenched POX stream below atemperature as defined herein and is sufficiently low to ensure that thevapor phase concentration of any inorganic components in the solid fuelis likewise sufficiently low to substantially prevent deposition in oneor more components of the power production system. For example, partialoxidation of coal can produce one or more alkali metal salts includingNaCl, CaSO₄, and KCl, which can be removed as discussed herein. Theupper temperature limit of the quenched POX stream also can be adaptedto ensure that the BOUDOUARD reaction is sufficiently slow so as tosubstantially prevent carbon deposition and/or metal dusting corrosionin any heat exchanger or other components in the power productionsystem.

The systems and methods of the present disclosure can be adapted toprovide for recovery of substantially all of the heat released duringcooling of the POX stream, preferably cooling to near ambienttemperature, and recovery of the heat into the recycled high pressureCO₂ stream in the power production system. This additional heatingparticularly can be provided at the lower temperature level in therecuperator heat exchanger of the power production system. Input ofadditional heat in this manner can provide a significant positive effecton the overall efficiency of the power production system. This effect isdue to the much higher specific heat of the high pressure recycle CO₂stream in the lower temperature range of 50° C. to 400° C. compared tothe higher temperature range of 400° C. to 800° C. and to the lowerspecific heat of the turbine exhaust stream that is cooling in therecuperator heat exchanger of the power production system. This markeddifference means that significant additional extra heat is required inthe recuperator heat exchanger over the temperature range 50° C. to 400°C. to heat the recycle CO₂ stream. The additional heat obtained from thequenched POX stream in the POX stream heat exchanger provides aneffective quantity of additional heat for the power production systemcombustor that is substantially equivalent to the quantity of heatreleased when fuel gas itself is combusted.

In various embodiments wherein the POX reactor is quenched to saturationusing a recycle water stream, the temperature-heat release curve for thequenched POX stream cooling to near ambient temperature shows a largeinitial heat release as the water vapor derived from vaporization of thequench water begins to condense. This heat release per unit temperaturedrop reduces progressively as the POX stream cools. The effect requirestwo separate high pressure recycle CO₂ streams taken from the powerproduction system high pressure recycle stream to be used to recoverheat from the cooling quenched POX stream. In some embodiments, thefirst high pressure recycle CO₂ stream can be taken from the CO₂ recyclecompressor discharge at the temperature of about 45° C. to about 70° C.The second high pressure recycle CO₂ stream can be taken from the highpressure recycle stream at a point in the recuperator heat exchangerwhere there is a small temperature approach to the dew-point of theturbine exhaust cooling stream. These two streams together can providefor a large initial heat release from the cooling quenched POX stream asits water content begins to condense that can be efficiently transferredback to the high pressure CO₂ recycle stream at the highest possibletemperature level (see FIG. 3). In embodiments wherein the POX stream isinitially quenched to about 400° C., a cooling range between about 400°C. and the water dew point of the quenched POX stream exists, and thisrange can require a lower flow of recycle high pressure CO₂ toefficiently remove this portion of the heat available from the quenchedPOX stream as compared to the temperature range below the water dewpoint of the POX stream. This can be accomplished by removing a portionof the heating high pressure recycle CO₂ stream at a point near and/orbelow the water dew-point temperature of the quenched POX stream whilethe remaining portion is removed at a temperature near to and/or belowthe quench temperature (e.g., about 400° C.) (see FIG. 4). The heatedhigh pressure recycle CO₂ streams then can be returned to therecuperator heat exchanger at a corresponding temperature point to thebulk flow of high pressure recycle CO₂ in the recuperator heatexchanger. In various embodiments, options for the two streams tocombine in the POX cooling heat exchanger with a single return streamcan be provided. In some embodiments, more than two streams of highpressure recycle fluid can be used.

In some embodiments, the fuel gas taken from the POX reactor followingquench and ash removal can comprise predominantly H₂, CO, CO₂ and H₂O ata temperature of about 250° C. to about 400° C. A portion of this fuelgas stream can be taken for the production of pure H₂, CO, or acombination thereof with varying H₂ to CO ratios. Typical applicationsfor large scale H₂ production can be, for example, hydro-desulfurizationand hydrocracking in refineries and, potentially, as a vehicle fuel.Typical applications for H₂ and CO mixtures can be, for example,Fischer-Tropsch hydrocarbon liquids production (e.g., with about a 2.2H₂ to CO ratio) and methanol production (e.g., with about a 2.0 H₂ to COratio). In each case, the H₂ to CO ratio must be increased from theratio of approximately 1 or less in the POX fuel gas stream where theratio depends on use of CO₂ or water as the slurrying medium for thesolid fuel. Water based slurry with more water in the POX product gasresults in a significant proportion of the CO being converted to H₂ andCO₂, giving a H₂ to CO ratio of just below 1. CO₂ based slurry has amuch lower H₂ to CO ratio. It can be useful to pass at least part of theseparated quenched POX fuel gas stream through a catalytic shift reactorto convert CO to H₂ by reaction with steam, as shown below in Formula(2).

CO+H₂O═H₂+CO₂  (2)

This can be accomplished using a portion of the fuel gas taken at atemperature of about 250° C. to about 400° C. following ash removal andby using a sulfur tolerant CO shift catalyst, such as one based oncobalt in the shift reactor. The portion of fuel gas that has beenenriched in H₂ can be then cooled in a separate pass through the POXheat exchanger. Heat released in the exothermic shift reaction can betransferred into the PPS as previously described. The exit shifted gasthen can be mixed with a portion of the remaining cooled POX stream andthe combined stream can be passed through a multi-bed pressure swingadsorber designed to separate the H₂ and CO at the required H₂ to COratio as a single non adsorbed component while the adsorbed componentscan contain all of the sulfur compounds, HCN, NH₃, Hg, CO₂, H₂O and mostof the CH₄. This un-adsorbed fraction may also contain some N₂ and Arderived from the coal (or other solid or liquid fuel) and oxygen used inthe POX reactor. These inert components preferably will be below 5%total concentration which is acceptable for the gas feed to both theFischer-Tropsch and Methanol reactors. If pure H₂ production isrequired, only the shifted cooled gas will be fed to the PSA. The nearatmospheric pressure waste gas from the PSA with all of the coal and POXderived impurities in a reduced form will be compressed and returned tothe remaining POX fuel gas for combustion in the PPS combustor.

One embodiment of a power production system with partial oxidation of asolid fuel is described in reference to FIG. 1, wherein a solid fuel isprovided in the form of coal feed stream 21 to be partially oxidized inthe POX reactor 4. The coal stream 21 is crushed and partially dried inlarge particle crusher 1 that is also fed dry nitrogen stream 23comprising N₂ at a temperature of about 82° C. (180° F.) taken from anair separation unit 6, which produces oxygen streams 32 and 60 andnitrogen stream 23 from air intake stream 62. Preferably, the drynitrogen stream 23 can be heated against a higher temperature stream ofCO₂ rich turbine exhaust leaving the recuperator heat exchanger in thePPS. The coal is further crushed to a particle size preferably of about250 microns or less in the small particle crusher 2 to provideparticularized coal stream 25, which is directed to a slurry mixer 3. Inthe slurry mixer 3, the particularized coal is mixed with CO₂ slurrymedium stream 29, which preferably has a pressure of about 8.5 MPa orgreater. The CO₂ in the CO₂ slurry medium stream 29 in this embodimentis at a temperature of about 17° C. The CO₂ in the CO₂ slurry mediumstream 29 has a density of about 865 kg/m³. The powdered coal isincreased in pressure in a lock hopper system or by other means to apressure of 8.5 MPa prior to mixing with the CO₂. A coal/CO₂ slurrystream 26 exits the slurry mixer 3 and preferably comprises about 45% byweight coal. Alternatively the slurry medium can be a water stream. Thepowdered coal injection system can also be configured as a dry feedsystem in which the powdered pressurized coal is entrained in a nitrogenstream and fed into the POX burner. The slurry stream 26 is then pumpedinto the POX reactor 4 where it is combined with oxygen stream 56, whichpreferably comprises 97% molar or greater oxygen concentration. The POXreactor 4 preferably operates at a pressure of about 8.5 MPa and atemperature of about 1400° C.; however, the temperature and pressure canbe in any combinations of temperature and pressure ranges as otherwisedisclosed herein in relation to the nature of the POX stream exiting thePOX reactor. The conditions for the preparation of the coal slurry canbe adjusted accordingly.

The POX reactor 4 is adapted to partially oxidize the coal and form aPOX stream, which may exit the POX reactor and enter a quench chamber(not illustrated) or may be quenched within the POX reactor itself, asillustrated in FIG. 1. The POX stream can comprise a fuel gas that cancomprise one or more combustible (i.e., oxidizable) materials, includingbut not limited to H₂, CO, CH₄, H₂S, COS, CS₂, HCN, NH₃. Moreover, thePOX stream can comprise Hg and other impurities derived from the coal(or other solid fuel) as well as inert materials (e.g., N₂ and Ar), suchas derived from the oxygen stream 56, plus other trace components. ThePOX stream also can comprise one or more non-combustible materials, suchas ash or slag, which can be filtered from the POX stream as desired.

The POX stream (either internal to the POX reactor or in a separatecomponent) is quenched by mixing with a quench fluid (liquid waterstream 57 in the present embodiment). As illustrated, the liquid waterstream 57 enters the POX reactor near the base in a restriction nozzle.The addition of the quench stream cools the POX stream componentspreferably to below the water saturation temperature of about 304° C.(although higher temperatures also are encompassed). The quenchtemperature preferably also can be a temperature at whichnon-combustibles, such as ash and slag, are in solid form. The excessquench water collects with the slag and the bulk of the fine ash in thesump of the POX reactor vessel (or separate quench vessel) where it isremoved for further treatment. The quenched POX stream 58 passes toscrubber unit 5, which comprises a water scrub tower followed by a finecartridge filter adapted to reduce the dust load to about 4 mg/m³ orless of fuel gas, about 3 mg/m³ or less of fuel gas, or about 2 mg/m³ orless of fuel gas. Scrubber unit 5 also can include all equipment andpumps required to recycle the scrub water and also to treat the ashstream 66 for disposal. An exemplary embodiment of a system useful forPOX reactor ash treatment and gas cleaning is a GE/Texaco POX systemwith a coal/water slurry burner, which alternatively can be modified toaccept a coal/CO₂ slurry.

The cleaned fuel gas plus steam stream 55 is cooled in heat exchanger 7.The exit stream 59 is further cooled against cooling water in heatexchanger 9. Liquid water 46 is separated in separation vessel 8 fromthe inlet stream 61 and pumped in pump 11 back to the POX reactor quenchand some addition makeup water from stream 38 to produce quench waterstream 57. The net fuel gas stream 47 is compressed in a multi-stagecentrifugal compressor 10 to a pressure suitable for input as stream 48to the power production system combustor 14. As an example, the fuel gasstream 47 can be compressed to a pressure of about 30.5 MPa. Thecompressed fuel gas stream 48 is heated in the recuperator heatexchanger 12 to a temperature suitable for input to the power productionsystem combustor 14. As an example, the compressed fuel gas stream 48can be heated to a temperature of about 746° C. The heated fuel gasstream 64 is burned in the power production system combustor 14 where itis combined with oxygen and CO₂. In the illustrated embodiment, combinedO₂/CO₂ stream 51 comprises 30% O₂ and 70% CO₂ on a molar basis. Thecombined O₂/CO₂ stream 51 preferably been heated to a temperaturesuitable for input to the power production system combustor 14. As anexample, the combined O₂/CO₂ stream 51 can be heated to a temperature ofabout 746° C. in the recuperator heat exchanger 12. A hot recycle CO₂stream 52 is directed from the recuperator heat exchanger 12 and is at atemperature suitable for input to the power production system combustor14. As an example, the hot recycle CO₂ stream 52 can be heated to atemperature of about 746° C.

In the power production system combustor, the combustion gases fromburning of the fuel gas are cooled with the hot recycle CO₂ stream 52producing a combined combustion product stream 50 at a temperature ofabout 1150° C. and a pressure of about 30 MPa in the illustratedembodiment. This is expanded to a pressure of about 3 MPa in turbine 13coupled to an electric generator 65 producing an output power 63. Theturbine outlet stream 49 is cooled in the recuperator heat exchanger 12leaving as cooled product stream 53 at a temperature of about 64° C. inthe illustrated embodiment. The stream 53 is cooled to a temperature ofabout 17° C. in water cooler 16. The further cooled turbine outletstream 54 enters a scrub tower 17, which has an outlet stream 40 that islargely recycled via circulation pump 18 to scrub tower liquid inlet 41above the packed section of the tower that receives the further cooledturbine outlet stream 54. A portion of stream 40 is split out as stream39 for further treatment. As the turbine exhaust gas cools below thewater dew-point in the recuperator heat exchanger 12 the followingreactions occur.

NO+½O₂═NO  (3)

NO₂+SO₂═SO₃+NO  (4)

SO₃+H₂O═H₂SO₄  (5)

The above reactions will proceed in the presence of liquid water,nitrogen oxides, SO₂/SO₃, and excess oxygen. The SO₂/SO₃ concentrationsare reduced to very low levels since the limiting reaction shown inFormula (3) rapidly proceeds at 3 MPa, and the reactions of Formula (4)and Formula (5) are very fast. When all of the sulfur oxides have beenconverted to sulfuric acid, the nitrogen oxides are converted at about95% conversion rate per pass to nitric acid with the following reactionsequence.

2NO₂+H₂O═HNO₂+HNO₃  (6)

3HNO₂═HNO₃+2NO+H₂O  (7)

NO+½O₂═NO₂  (8)

Returning to FIG. 1, the nitric acid present in net liquid acid productstream 39 will convert any mercury present to mercuric-chloride. Thescrub tower 17 preferably is fitted with an additional water wash andacid mist removal section. Its primary function is to act as anefficient dilute acid removal device since virtually all the abovereactions will have taken place upstream of the scrub tower 17. Themixed acids are treated with limestone slurry stream 36 (or othersuitable base) in mixer 15 to produce gypsum and calcium nitrate stream37. Any other trace metallic salts can also be separated. The residualwater stream 38 following calcium nitrate and dissolved salts removalcan be used as make-up to a cooling tower or the POX quench system or asscrub water recycled to scrub tower 17.

The predominantly CO₂ stream 42 leaving the scrub tower 17 at a pressureof about 2.9 MPa is compressed in a multi-stage intercooled compressor19 followed by a dense fluid multistage pump to a pressure suitable forinput to the power production system combustor, such as about 30.5 MPa.The compressed CO₂ discharge stream 35 leaves the last stage of the pump19 at a temperature of about 54° C., and part of this flow, stream 70,is heated in the recuperator heat exchanger 12 to a temperature of about746° C., leaving as CO₂ stream 52.

The air separation plant 6 in this embodiment produces a 99.5% molaroxygen purity product stream at a pressure of about 8.6 MPa whichdivides into two separate streams. Oxygen stream 60 is heated in heatexchanger 7 to a temperature of about 294° C., exiting as stream 56 foruse in the POX reactor 4 for partial oxidation of the coal. Theremaining oxygen stream 32 is mixed with CO₂ at a pressure of about 8.6MPa. Specifically, CO₂ is taken from an intermediate stage of thecompressor 19 as stream 30, and a portion stream 31 mixes with oxygenstream 32 giving a composition of about 30% O₂ and 70% CO₂ molar. Thisdiluted O₂ stream 33 is compressed to a pressure of about 30.5 MPa in amulti-stage intercooled compressor 20 and the discharge stream 34 isheated in the recuperator heat exchanger 12 to a temperature of about746° C. and enters the power production system combustor 14 as stream51. Dilution of the pure O₂ stream 32 is beneficial to allow the oxygenrequired for combustion in the power production system combustor 14 tobe heated to a high temperature without the need for oxidation resistantmaterials. This ensures the safe operation of the power productionsystem. The 30% O₂ stream is useful to moderate the adiabatic combustiontemperature in power production system 14 to a value of approximately2400° C. The remaining portion of CO₂ stream 30 is CO₂ stream 29, whichprovides the CO₂ for slurrying the powdered coal and is directed toslurry mixer 3.

Cooling of the quenched POX gas in heat exchanger 7 is useful totransfer the maximum quantity of heat to the power production system tomaximize the overall efficiency. The power production system requires asignificant quantity of heat from an external source in the temperaturerange from near ambient up to about 400° C. This can be provided byusing adiabatic air compressors in the air separation plant 6 andtransferring the heat of compression to part of the high pressurerecycle CO₂ stream. In the present embodiment, the required externalheating load is provided by cooling the quenched POX gas in heatexchanger 7 and heating two high pressure recycle streams. High pressurerecycle CO₂ stream 28 at a temperature of about 54° C. and high pressurerecycle CO₂ stream 43 at a temperature of about 120° C. taken from anintermediate temperature point in recuperator heat exchanger 12 areheated to provide a combined heating outlet stream 44 at a temperatureof about 294° C., which is returned to mix with the main recycle CO₂stream at a corresponding temperature point in recuperator heatexchanger 12. Optionally, outlet stream 67 also may be returned to therecuperator heat exchanger at a corresponding temperature point to mixwith the main recycle CO₂ stream as well.

Illustrated in FIG. 3 is a plot of temperature against percentage heatrelease (diagrammatically) in the recuperator heat exchanger 7 of FIG. 1to show the benefit of two separate inlet streams of high pressurerecycle CO₂ to ensure efficient operation of the combined system. The120° C. temperature level of stream 43 inlet corresponds to atemperature approach to the water dew-point of the turbine exhauststream in recuperator heat exchanger 12. The quenched POX fuel gasenters the heat exchanger at the water saturation temperature of 304°C., and the total heated high pressure recycle stream leaves at atemperature of 294° C.

Shown in FIG. 4 is an alternative method of operation in which thequench water stream reduces the POX gas temperature to about 400° C.There is an additional section of heat exchanger in which the quenchedPOX fuel gas temperature falls to its dew-point of about 300° C. Tomaximize the efficiency of the total power production system byminimizing the temperature difference in heat exchanger 7, the highpressure heated CO₂ stream is removed from the heat exchanger as twoseparate streams. Stream 44 is at a temperature of about 290° C. andstream 67 is at a temperature of about 390° C. These streams areseparately returned to recuperator heat exchanger 12 where they reunitewith the main high pressure recycle CO₂ stream at the appropriatecorresponding temperatures.

In exemplary embodiments, heat exchanger 7 can be a high pressure brazedor diffusion bonded multi-channel unit. The material of constructionpreferably is corrosion resistant in the presence of the impuritiespresent in the POX gas plus liquid water. Recuperator heat exchanger 12preferably is a diffusion bonded multi-channel unit. This unitpreferably is adapted for operation at temperatures up to about 800° C.and to be resistant to acid corrosion at temperatures below about 200°C. An exemplary suitable material is Specialty Metals alloy 740. In someembodiments, the average temperature at the hot end of heat exchanger 12can be reduced to below 750° C. and, in such cases, alloy 617 can besuitable. Optionally the intermediate section between 200° C. and 540°C. can be fabricated from stainless steel. The section which is subjectto potential acid corrosion below 200° C. can be constructed to allowreplacement at intervals.

In further embodiments, alternate arrangements of the elements forprocessing the POX stream can be used. In an exemplary embodiment, FIG.2 shows an optional arrangement wherein the POX product is used both forproduction of fuel gas for the power production system and forproduction of a separated and purified mixture of H₂ and CO. Aside-stream 66 is taken from the quenched POX gas stream 55 followingash removal and passed through a catalytic shift converter 67 having asulfur resistant cobalt based shift catalyst (or other suitablematerial). The higher temperature exit gas stream 70 is cooled in heatexchanger 7 to a temperature of about 60° C., exits as stream 73, and isfurther cooled by cooling water in heat exchanger 74 to a temperature ofabout 20° C. as stream 75. Condensed water is separated in separator 77,and the cooled gas stream 76 enters a multi-bed pressure swingadsorption unit 79. The water separated in separator 77 is added toliquid water stream 46. The pressure swing adsorption unit (PSA) 79 isdesigned to separate the inlet gas stream 76 into a pure H₂ or a pure H₂and CO stream 80 leaving the unit at a pressure of about 8 MPa and awaste gas stream 71 which contains all of the impurities (e.g., H₂S,COS, CS₂, HCN, NH₃, Hg, and other trace components) as well as somecombination of H₂, CO, CO₂, CH₄, and H₂O. The separation of theimpurities is such that the concentration of these components in the H₂or H₂ and CO product stream 80 is below 1 ppm. This arrangement uses astream 83 of cooled POX gas containing a high concentration of CO toblend with the shifted cooled gas stream 76 to produce a stream 72 whichwhen passed through the PSA unit 79 and gives the required flow and therequired H₂ to CO ratio in the 8 MPa product stream 80. If pure H₂ isrequired then stream 83 is zero. The waste gas stream 71 from the PSA 79at 0.12 MPa pressure is compressed in a multi-stage intercooledcompressor 81 to a pressure of about 8 MPa, and the discharge stream 82is added to the power production system fuel gas stream 47. The totalfuel gas stream is compressed to a pressure of about 30.5 MPa incompressor 10, and the resultant high pressure fuel gas stream 48 issent to the power production system combustor 14 via recuperator heatexchanger 12 (referencing FIG. 1). This arrangement ensures the transferof all coal and POX derived impurities to the power production systemwhere they are oxidized in the power production system combustor 14. Invarious embodiments, the consumption of additional water in the shiftreaction can proceed according to Formula (9) and may require a smalladditional make-up flow.

H₂O+CO═CO₂+H₂  (9)

In various embodiments incorporating elements of the systems and methodsdescribed herein, the overall efficiency of the disclosed systems andmethods is greater than 50% (on a lower heating value (LHV) basis withrepresentative turbine and compressor efficiencies and heat exchangertemperature differences and pressure drops). Moreover, CCS issimultaneously provided along with substantially complete removal of allother fuel, POX, and combustion derived impurities. Excess CO₂ derivedfrom the carbon in the fuel stream 21 is removed from the circulatingCO₂ system as stream 71 at 30.5 MPa. This can be facilitated in that thesystems and methods can be adapted to provide substantially all of thefuel derived CO₂ at a pressure of about 15 MPa or greater, about 20 MPaor greater, about 25 MPa or greater, or about 30 MPa or greater. Thishigh efficiency beneficially can be achieved with a low cost system,such as using commercially available POX reactor systems and a highpressure CO₂ working fluid power cycle, such as described in U.S. PatentApplication Publication No. 2011/0179799, which is incorporated hereinby reference in its entirety. As a comparative example, existingcommercial coal based integrated gasification combined cycle (IGCC)power generation systems with CO₂ capture and compression to pipelinepressure have been shown to have efficiencies on a comparable basis ofonly 34% to 39% and have much higher capital cost.

EXPERIMENTAL

The above described advantages of the presently disclosed methods andsystems were verified via extensive ASPEN simulations under a variety ofconditions with realistic estimates for commercial equipmentperformance. Two sets of simulations were carried out using Illinois #6coal as the solid fuel introduced to the POX combustor. In each case,data is based upon the use of CO₂ as the coal slurry medium. Thesimulations differed in that the first simulation (see FIG. 5) was basedupon the use water as the quenching fluid, and the second simulation(see FIG. 6) was based upon the use of CO₂ as the quench fluid.

Details of the mass and heat balance from the first simulation areprovided in the Table shown in FIG. 5. Under the shown conditions, afuel gas was produced typically with a H₂ to CO ratio of 0.41 to 1. Thecalculated efficiency for this embodiment on a lower heating value (LHV)basis was 51.44%.

Details of the mass and heat balance from the second simulation areprovided in the Table shown in FIG. 6. Under the shown conditions, afuel gas was produced typically with a H₂ to CO ratio of 0.17 to 1. Ineach case, hydrogen ratios can be increased with embodiments using watershift. The calculated efficiency for this embodiment on a LHV basis was51.43%.

Many modifications and other embodiments of the presently disclosedsubject matter will come to mind to one skilled in the art to which thissubject matter pertains having the benefit of the teachings presented inthe foregoing descriptions and the associated drawings. Therefore, it isto be understood that the present disclosure is not to be limited to thespecific embodiments described herein and that modifications and otherembodiments are intended to be included within the scope of the appendedclaims. Although specific terms are employed herein, they are used in ageneric and descriptive sense only and not for purposes of limitation.

1. A process for the production of power using a combination of apartial oxidation (POX) system and a power production system (PPS), theprocess comprising: combining a solid or liquid fuel and oxygen in a POXreactor under conditions sufficient to partially oxidize the fuel andform a POX stream comprising a fuel gas; quenching the POX streamthrough combination with a quenching fluid under conditions sufficientto form a quenched POX stream at a temperature of about 400° C. or lessand to solidify at least a portion of any molten solids present in thePOX stream; treating the quenched POX stream so as to remove at least aportion of any solids present therein; directing the quenched POX streamto a POX heat exchanger and withdrawing a quantity of heat from thequenched POX stream by cooling the quenched POX stream to a temperatureof about 100° C. or less against a cooling stream and form a POX fuelgas stream; passing the POX fuel gas stream through a separator vesseland separating at least a portion of any water present in the POX fuelgas stream; compressing the POX fuel gas stream to a pressure of about12 MPa or greater; combusting the POX fuel gas in a PPS combustor toform a combustion product stream at a pressure of at least about 10 MPaand a temperature of at least about 800° C.; and expanding thecombustion product stream across a PPS turbine to generate power andform an expanded PPS combustion product stream.
 2. The process of claim1, wherein the solid or liquid fuel is a carbonaceous fuel.
 3. Theprocess of claim 2, wherein the fuel combined in the POX reactor is anentrained stream of a powdered, solid fuel.
 4. The process of claim 2,wherein the carbonaceous fuel is coal.
 5. The process of claim 4,wherein the coal is slurried with water or CO₂.
 6. The process of claim4, wherein the quenched POX stream comprises ash, slag, or a combinationthereof, and wherein the step of removing solids comprises passing thequenched POX stream through a water scrubber unit.
 7. The process ofclaim 4, wherein the step of removing solids comprises filtering thequenched POX stream so as to reduce dust load to about 4 mg or less percubic meter of fuel gas in the quenched POX stream.
 8. The process ofclaim 1, wherein the POX reactor is operated at a POX temperature, andwherein a ratio of the POX temperature to the temperature of thequenched POX stream is about 3.25 or greater.
 9. The process of claim 8,wherein the POX temperature is about 1300° C. to about 1600° C.
 10. Theprocess of claim 1, wherein the POX reactor is operated at a pressure ofabout 2 MPa or greater.
 11. The process of claim 1, wherein quenchingcomprises mixing the POX stream with: a recycled portion of the cooledPOX fuel gas stream exiting the heat exchanger; a portion of the waterseparated from the cooled POX fuel gas stream; a portion of a CO₂recycle stream from the PPS; or a combination thereof.
 12. The processof claim 1, wherein the cooling stream in the heat exchanger comprises ahigh pressure recycle fluid stream withdrawn from and returned to thePPS.
 13. The process of claim 12, wherein the high pressure recyclefluid stream is a recycle CO₂ fluid stream.
 14. The process of claim 13,wherein the recycle CO₂ fluid stream comprises CO₂ formed in thecombusting of the POX fuel gas in the PPS combustor.
 15. The process ofclaim 1, wherein the POX reactor includes an internal heat transfercomponent.
 16. The process of claim 15, wherein the internal heattransfer component is adapted to transfer radiant heat to a portion of ahigh pressure recycle stream taken from a component of the PPS at atemperature of about 250° C. or greater.
 17. The process of claim 16,wherein the internal heat transfer component is adapted to return thehigh pressure recycle stream to a component of the PPS.
 18. The processof claim 1, wherein the turbine has an inlet pressure of about 10 MPa orgreater.
 19. The process of claim 18, wherein the turbine has an outletpressure that is defined as a ratio of the turbine inlet to the turbineoutlet, said ratio being about 12 or less.
 20. The process of claim 1,wherein the oxygen used in the POX reactor has a purity of about 90%molar or greater.
 21. The process of claim 20, wherein the oxygen usedin the POX reactor has a purity of about 95% molar or greater.
 22. Theprocess of claim 1, further comprising: passing the expanded PPScombustion product stream through a PPS recuperator heat exchanger andthereby withdrawing heat from the PPS combustion product stream andforming a cooled PPS combustion product stream; optionally passing thecooled PPS combustion product stream through a water cooler; treatingthe cooled PPS combustion product stream in a PPS scrubber separating atleast H₂SO₄, HNO₃, or Hg and forming a recycle CO₂ stream; andpressurizing the recycle CO₂ stream in a PPS compressor and forming acompressed recycle CO₂ stream.
 23. The process of claim 22, whereinpassing the expanded PPS combustion product stream through the PPSrecuperator heat exchanger cools the PPS combustion product stream to atemperature below the water dew point.
 24. The process of claim 22,wherein the fuel gas in the POX fuel gas stream entering the PPScombustor comprises at least one fuel gas component selected from H₂,CO, and CH₄.
 25. The process of claim 24, wherein the POX fuel gasstream entering the PPS combustor comprises one or more impuritiesseparate from the fuel gas and derived from the solid or liquid fuel,the partial oxidation thereof, and the oxygen.
 26. The process of claim24, wherein the one or more impurities comprise at least one of a sulfurcompound, NH₃, and HCN.
 27. The process of claim 25, whereinsubstantially all of the impurities are still present in the POX fuelgas stream and are combusted in the PPS combustor.
 28. The process ofclaim 26, wherein all oxidizable impurities present in the POX fuel gasstream are oxidized by the combustion in the PPS combustor.
 29. Theprocess of claim 22, wherein the combustion product stream from the PPScombustor comprises a mixture of combustion products and at least aportion of the compressed recycle CO₂ stream.
 30. The process of claim22, wherein the withdrawn heat from the PPS combustion product streamheats at least a portion of the compressed recycle CO₂ stream.
 31. Theprocess of claim 22, wherein the POX stream is quenched with water. 32.The process of claim 31, wherein the water quenched POX stream comprisesat least H₂, CO, CO₂, H₂S, and H₂O.
 33. The process of claim 32, whereinthe cooling stream in the POX heat exchanger comprises two streams ofthe compressed recycle CO₂.
 34. The process of claim 33, wherein aninlet temperature of the first compressed recycle CO₂ stream enteringthe POX heat exchanger is substantially the same as a temperature of thecompressed recycle CO₂ stream discharged from the PPS compressor. 35.The process of claim 33, wherein an inlet temperature of the secondcompressed recycle CO₂ stream entering the POX heat exchanger is within20° C. of the water dew-point in the expanded PPS combustion processstream.
 36. The process of claim 35, wherein the water quenched POXstream is saturated with water vapor so as to comprise excess liquidwater.
 37. The process of claim 36, wherein the two compressed recycleCO₂ streams combine in the POX heat exchanger to form a single stream.38. The process of claim 37, wherein the single compressed recycle CO₂stream exiting the POX heat exchanger is at a temperature that is withinabout 20° C. of the POX fuel gas dew-point temperature.
 39. The processof claim 37, wherein the water quenched POX stream has a temperaturethat is above its dew-point temperature and below about 400° C.
 40. Theprocess of claim 39, wherein the two compressed recycle CO₂ streams areheated, and wherein the point at which the two compressed recycle CO₂streams combine to form the single stream is at a temperature thatsubstantially corresponds to the inlet temperature of the secondcompressed recycle CO₂ stream.
 41. The process of claim 40, wherein thesingle stream is split into: a first exiting heated and compressedrecycle CO₂ stream that exits the POX heat exchanger at a temperaturethat is within about 20° C. of the POX stream dew-point temperature; anda second exiting heated and compressed recycle CO₂ stream that exits thePOX heat exchanger at a temperature of about 380° C. to about 399° C.42. The process of claim 22 wherein the POX stream is quenched with CO₂and optionally a portion of the fuel gas.
 43. The process of claim 42wherein the CO₂ quenched POX stream comprises at least H₂, CO, CO₂, H₂S,and H₂O.
 44. The process of claim 43, wherein the cooling stream in thePOX heat exchanger comprises one stream of the compressed recycle CO₂.45. The process of claim 44 wherein an inlet temperature of thecompressed recycle CO₂ stream entering the POX heat exchanger issubstantially the same as a temperature of the compressed recycle CO₂stream discharged from the PPS compressor and the single compressedrecycle CO₂ stream exiting the POX heat exchanger is at a temperaturethat is within about 20° C. of the POX fuel gas dew-point temperature.46. The process of claim 22, wherein at least a portion of the waterquenched POX fuel gas enters a catalytic shift reactor adapted toconvert a mixture of CO and H₂O into a shift reactor exit gas comprisinga mixture of H₂ and CO₂.
 47. The process of claim 46, wherein the shiftreactor exit gas is cooled in the POX heat exchanger against a highpressure recycle CO₂ gas taken from and returned to the PPS.
 48. Theprocess of claim 47, wherein the shift reactor exit gas is cooled in thePOX heat exchanger and mixed with a portion of the quenched POX streamwhich has been cooled in the heat exchanger and is further processed toseparate water, CO₂, sulfur compounds, nitrogen compounds, and Hg, so asto form a mixture comprising H₂ and CO in a ratio of about 0.8:1 toabout 2.5:1.
 49. The process of claim 48, wherein the cooled shiftreactor exit gas is further processed to form a pure H₂ stream with apurity of 99% or greater molar.
 50. The process of claim 48, wherein thePOX catalytic shift reactor is a multi-bed pressure swing adsorption(PSA) system.
 51. The process of claim 50, wherein a low pressure wastegas from the PSA system comprising adsorbed products from the PSA systemis compressed to a PPS combustor pressure and mixed into a total fuelgas flow entering the PPS combustor.
 52. The process of claim 22,wherein the oxygen used in the POX reactor is heated in the POX heatexchanger to a temperature of up to about 350° C.
 53. The process ofclaim 22, wherein the oxygen used in the PPS combustor is heated in thePOX heat exchanger to a temperature of about 350° C.
 54. A combinedpartial oxidation (POX) system and power production system (PPS)comprising: a POX reactor adapted to partially oxidize a liquid or solidfuel in the presence of oxygen to form a POX stream comprising a fuelgas; one or more components adapted to contact the POX stream with aquenching fluid; an optional POX scrubber adapted to separate any solidspresent in the quenched POX stream from the POX fuel gas; an optionalfiltration device adapted to separate solidified ash particle from asingle phase quenched POX fuel gas stream a POX heat exchanger adaptedto withdraw heat from the POX fuel gas against a portion of a compressedrecycle CO₂ stream and output a cooled POX fuel gas; an optionalseparator adapted to separate any liquid water from the POX fuel gas; acompressor adapted to compress the cooled POX fuel gas to a pressure ofabout 10 MPa or greater; a PPS combustor adapted to combust the POX fuelgas in the presence of oxygen and a portion of the compressed recycleCO₂ stream and form a PPS combustion product stream at a pressure ofabout 10 MPa or greater; a turbine adapted to expand the PPS combustionproduct stream and generate power in a connected generator; arecuperator heat exchanger adapted to withdraw heat from the expandedPPS combustion product stream and add the heat to the compressed recycleCO₂ stream; a PPS scrubbing tower adapted to separate one or more ofH₂SO₄, HNO₃, and water-dissolved Hg salts from the expanded PPScombustion product stream and output a recycle CO₂ stream; a PPScompressor adapted to compress the recycle CO₂ stream to a pressure ofabout 10 MPa or greater and form the compressed recycle CO₂ stream; flowcomponents adapted to direct a portion of the compressed recycle CO₂stream to the POX heat exchanger; flow components adapted to direct aportion of the compressed recycle CO₂ stream to the PPS recuperator heatexchanger; and flow components adapted to direct the compressed recycleCO₂ stream from the POX heat exchanger to the PPS recuperator heatexchanger.